A gasoline refining method and system

Abstract

The present application relates to a gasoline refining method, which comprises: cutting gasoline into light fraction, middle fraction and heavy fraction, respectively carrying out adsorption desulfurization and hydrorefining reaction in two moving bed reactors, removing the deactivated catalyst from the reactor to the regeneration system to recover the activity, and then returning it to the reactor in a continuous manner to realize the continuous circulation of the reaction-regeneration process. The method can deeply remove sulfur and nitrogen impurities in hydrocarbon oil, completely saturate and remove olefins contained therein while reducing or even increasing the loss of aromatic hydrocarbons. The regeneration problem of the deactivated catalyst is solved, the stability of the catalyst in the reaction process is improved, and the requirement for the catalyst wear index is greatly reduced.

Description

Technical Field

[0001] This invention belongs to the field of petroleum processing technology and relates to a method and system for refining gasoline using a moving bed. Background Technology

[0002] Aromatics, as one of the most important basic raw materials for petrochemical products, are widely used in chemical, agricultural, and pharmaceutical fields. One of the main sources of aromatics is the extraction and separation of catalytic reforming gasoline and cracked gasoline produced in ethylene plants. The catalytic cracking (DCC) technology developed by the Sinopec Research Institute of Petroleum Processing, which produces a high propylene yield from heavy feedstock, generates a high content of aromatics in the byproduct DCC gasoline. This byproduct can be used to produce aromatics through an aromatics extraction process. However, DCC gasoline has a high olefin content and contains impurities such as sulfur and nitrogen. Aromatics extraction feedstock requires a sulfur mass fraction of less than 1 μg / g, a nitrogen mass fraction of less than 1 μg / g, and a bromine value of less than 0.5 gBr / 100g. Therefore, before using the extraction process, DCC gasoline must undergo hydrorefining to saturate olefins and remove sulfur and nitrogen impurities.

[0003] Traditional hydrodesulfurization processes result in significant aromatic hydrocarbon losses during deep hydrodesulfurization of gasoline. CN200810224665.5 discloses a hydrotreating method for producing aromatic hydrocarbon extraction feedstock. This method employs two hydrotreating units, conducting different reactions at different temperatures. The first hydrotreating unit is loaded with a protective agent and removes dienes at a lower temperature. The second hydrotreating unit is loaded with a hydrorefining catalyst and performs desulfurization, denitrogenation, and olefin saturation at a higher temperature, while minimizing aromatic hydrocarbon saturation. Using this method, aromatic hydrocarbon extraction feedstock with sulfur and nitrogen contents both less than 1 μg / g and a bromine value less than 0.5 gBr / 100g can be produced. Summary of the Invention

[0004] The main technical problem to be solved by this invention is to provide a new moving bed method for gasoline refining, which combines a moving bed hydrorefining reactor with a moving bed hydrorefining catalyst regeneration system. This achieves continuous production of hydrorefining reaction-catalyst regeneration and reduction, while improving the stability of catalyst activity and the effective regeneration of catalyst during the reaction process.

[0005] A first aspect of the present invention provides a method for refining gasoline, comprising:

[0006] (1) The gasoline raw material is cut into light gasoline, medium gasoline and heavy gasoline. The first cutting point for cutting light gasoline and medium gasoline is 50-90℃, and the second cutting point for cutting medium gasoline and heavy gasoline is 130-150℃. The light gasoline and heavy gasoline obtained from the cutting are the first gasoline raw material, and the medium gasoline is the second gasoline raw material.

[0007] (2) The mixture of the first gasoline feedstock and hydrogen is fed into the first moving bed reactor filled with an adsorption desulfurization catalyst for desulfurization adsorption and hydrogenation refining to obtain the first oil and gas product. The mixture of the second gasoline feedstock and hydrogen is fed into the second moving bed reactor filled with an adsorption desulfurization catalyst for desulfurization adsorption and hydrogenation refining to obtain the second oil and gas product.

[0008] (3) The first oil and gas product and the second oil and gas product are introduced into the oil and gas separation device separately or together to separate the gas product and obtain the liquid refined gasoline product.

[0009] (4) The desulfurization catalyst to be regenerated after the reaction in the first moving bed reactor is introduced into the first regenerator for regeneration and reduction to obtain the first regenerated catalyst, and the first regenerated catalyst is returned to the first moving bed reactor; the desulfurization catalyst to be regenerated after the reaction in the second moving bed reactor is introduced into the second regenerator for regeneration and reduction to obtain the second regenerated catalyst, and the second regenerated catalyst is returned to the second moving bed reactor.

[0010] According to the method of the first aspect, in step (1), the sulfur content of the gasoline feedstock is above 10 micrograms / gram, preferably above 30 micrograms / gram;

[0011] The nitrogen content is above 10 micrograms / gram, preferably above 20 micrograms / gram;

[0012] The olefin mass fraction is 5%-50%, preferably 10%-45%;

[0013] The aromatic hydrocarbon mass fraction is above 20%-90%, preferably 30%-80%;

[0014] Preferably, the gasoline feedstock is selected from one or more of catalytic cracking gasoline, reformed gasoline, or steam cracking gasoline.

[0015] According to the method of the first aspect, in step (2), the first gasoline feedstock, the second gasoline feedstock and / or hydrogen are preheated before entering the moving bed reactor, and the preheating temperature is 200-550°C.

[0016] According to the method of the first aspect, in step (2), the reaction conditions in the first moving bed reactor are: reaction temperature of 350–550℃, reaction pressure of 0.5–5 MPa, and weight hourly space velocity of 0.1–100.0 h⁻¹. -1 The adsorption desulfurization catalyst moves at a velocity of 0.02–5.00 m / h in the first moving bed reactor, and the molar ratio of hydrogen to the first gasoline feedstock is 0.2–20.0; and / or

[0017] The reaction conditions in the second moving bed reactor are: reaction temperature 300–450℃, reaction pressure 1.5–5 MPa, and weight hourly space velocity 0.1–100.0 h⁻¹.-1 The adsorption desulfurization catalyst moves at a speed of 0.02–5.00 m / h in the second moving bed reactor, and the molar ratio of hydrogen to the first gasoline feedstock is 0.2–20.0.

[0018] According to the method of the first aspect, in step (3), the oil-gas separation temperature in the first oil-gas separation device is 30-150°C, and the oil-gas separation pressure is 0.5-4 MPa; and / or

[0019] The oil-gas separation temperature in the second oil-gas separation device is 50–200℃, and the oil-gas separation pressure is 0.5–4MPa.

[0020] According to the method of the first aspect, in step (4), the regeneration conditions of the first regenerator and / or the second regenerator are as follows:

[0021] The regeneration temperature is 300–550℃, and the regeneration pressure is 0.1–2.0 MPa.

[0022] Preferably, the oxygen volume content in the regenerated gas is 0.1% to 21.0%, and air is preferred.

[0023] According to the method of the first aspect, in step (4), the reduction conditions of the first regenerator and / or the second regenerator are:

[0024] The reduction temperature is 260–450℃, and the reduction pressure is 0.1–2.0 MPa;

[0025] Preferably, the hydrogen volume content in the reducing gas is at least 40%.

[0026] According to the method of the first aspect, in step (2), the adsorption desulfurization catalyst includes a support and a transition metal active component supported on the support;

[0027] Preferably, the support comprises zinc oxide, alumina, silica, and molecular sieve; and / or the transition metal active component is selected from one or more of cobalt, nickel, iron, manganese, copper, molybdenum, tungsten, silver, tin, and vanadium;

[0028] More preferably, the support contains 20-85 wt% zinc oxide, 5-85 wt% alumina, 5-85 wt% silica, and 5-35 wt% molecular sieve; the content of the transition metal active component accounts for 5-30 wt% of the total weight of the hydrorefining catalyst.

[0029] More preferably, the molecular sieve is a ZSM series molecular sieve, a Y-type molecular sieve, or a Beta-type molecular sieve;

[0030] More preferably, the molecular sieve is one in which Na has been replaced by ammonia exchange. +Ions, and molecular sieves that have been calcined at 450-700℃ for 1-10 hours.

[0031] A second aspect of the present invention provides a gasoline refining system, comprising:

[0032] The raw material cutting unit includes:

[0033] A gasoline cutting tower is used to cut gasoline feedstock into light gasoline, medium gasoline and heavy gasoline. It is equipped with a gasoline feedstock inlet, a light gasoline outlet, a medium gasoline outlet and a heavy gasoline outlet.

[0034] The reaction unit includes:

[0035] The first moving bed reactor is used to desulfurize, adsorb, and hydrogenate light gasoline and heavy gasoline to obtain the first oil and gas product. It is provided with a first gasoline feedstock inlet, a first oil and gas product outlet, a first spent catalyst outlet, and a first regenerated catalyst inlet. The first gasoline feedstock inlet is connected to the light gasoline outlet and the heavy gasoline outlet of the gasoline cutting tower.

[0036] The second moving bed reactor is used to desulfurize and adsorb hydrogenate the intermediate gasoline to obtain the second oil and gas product. It is equipped with a second gasoline feedstock inlet, a second oil and gas product outlet, a second unused catalyst outlet, and a second unused catalyst inlet. The second gasoline feedstock inlet is connected to the intermediate gasoline outlet of the gasoline cutting tower.

[0037] The oil-gas separation unit includes:

[0038] One or more oil-gas separation devices are used to separate a first oil-gas product and a second oil-gas product. The device is provided with an oil-gas product inlet, a gas product outlet and a liquid product outlet. The oil-gas product inlet is connected to the first oil-gas product outlet of the first moving bed reactor and the second oil-gas product outlet of the second moving bed reactor.

[0039] An optional mixer is used to mix liquid products from multiple oil-gas separation units to obtain refined gasoline products, the mixer being connected to the liquid product outlet of the oil-gas separation unit.

[0040] According to the system of the second aspect, the raw material cutting unit further includes an optional raw material mixer for mixing light gasoline and heavy gasoline as a first gasoline raw material.

[0041] According to the system of the second aspect, the first moving bed reactor and / or the second moving bed reactor are axial moving bed reactors, in which the gasoline feedstock and hydrogen mixture undergo adsorption desulfurization and hydrorefining reaction with the adsorption desulfurization catalyst through co-current or counter-current contact.

[0042] According to the system of the second aspect, the first moving bed reactor and / or the second moving bed reactor are radial moving bed reactors;

[0043] Preferably, the radially moving bed reactor is cylindrical, with a central tube, an inner annular tube, and an outer annular tube arranged radially outward from its central axis. The inner annular gap between the inner annular tube and the central tube is the catalyst moving bed, and the outer annular gap between the outer annular tube and the inner annular tube is the reactant channel. The central tube is the product channel, allowing gasoline feedstock and hydrogen to mix and enter through the reactant channel. The mixture then enters through the reactant channel and undergoes cross-flow contact with the catalyst moving downward in the catalyst moving bed along the radial direction of the reactor, resulting in an adsorption desulfurization and hydrorefining reaction. The reacted oil and gas enter the central tube and are then drawn out.

[0044] According to the system of the second aspect, a catalyst moving bed is provided in the middle of the first moving bed reactor and / or the second moving bed reactor, and a reactant channel is provided on one side of the catalyst moving bed and a product channel is provided on the other side, so that the mixture of gasoline feedstock and hydrogen enters from the reactant channel, enters the reactor laterally, and undergoes adsorption desulfurization reaction by cross-flow contact with the catalyst moving downward in the catalyst moving bed, and the gasoline after reaction is drawn out from the product channel.

[0045] According to the system of the second aspect, the reaction unit further includes at least one heating device for heating the first gasoline feedstock, the second gasoline feedstock, and / or hydrogen.

[0046] According to the system of the second aspect, the first moving bed reactor and / or the second moving bed reactor are single-stage or multi-stage reactors;

[0047] Preferably, the first moving bed reactor and / or the second moving bed reactor are multi-stage reactors, wherein the multi-stage reactors are connected in series, parallel or mixed.

[0048] More preferably, when the multi-stage reactors are connected in series, the multi-stage reactors are arranged horizontally side by side or vertically overlapping.

[0049] The gasoline refining method provided by this invention has, but is not limited to, the following beneficial effects:

[0050] (1) The present invention removes heteroatoms from high-olefin and high-aromatic hydrocarbon oils by hydrorefining reaction in a moving bed reactor, achieving deep desulfurization, denitrogenation and olefin reduction of hydrocarbon oils while minimizing or even increasing aromatic loss.

[0051] (2) The present invention cuts gasoline feedstock into different moving bed reactors and removes heteroatoms from high-olefin and high-aromatic hydrocarbon oils through hydrorefining reaction. While achieving deep desulfurization, denitrogenation and olefin reduction of hydrocarbon oils, the loss of aromatics is small or even increased.

[0052] (3) The present invention significantly reduces the amount of aromatic saturation and hydrogen consumption, thereby reducing costs and significantly reducing direct or indirect carbon emissions from the process.

[0053] (4) This invention maximizes the reaction on the basis of making full use of catalyst activity, and can realize the continuous process of hydrogen refining reaction-catalyst regeneration and reduction, while maximizing the deep desulfurization, denitrogenation and olefin reduction of gasoline, while minimizing or even increasing the loss of aromatics. Attached Figure Description

[0054] Figure 1 A flowchart of a specific embodiment of the present invention (two gas separation devices) is shown.

[0055] Figure 2 A flowchart of a specific embodiment of the present invention (a gas separation device) is shown.

[0056] Explanation of reference numerals in the attached figures:

[0057] 1. Gasoline feedstock; 2. Gasoline cutting tower; 3. Light gasoline; 4. Medium gasoline; 5. Heavy gasoline; 6. First hydrogen source; 7. Second hydrogen source; 8. First moving bed reactor; 9. Second moving bed reactor; 10. First regenerator; 11. Second regenerator; 12. First high-pressure separator; 13. Second high-pressure separator; 14. First liquid product; 15. Second liquid product; 16. Mixer; 17. Refined gasoline; 18. First pre-regenerating agent; 19. First regenerating agent; 20. Second pre-regenerating agent; 21. Second regenerating agent; 22. First oil and gas product; 23. First gaseous product; 24. Second oil and gas product; 25. Second gaseous product; 26. High-pressure separator; 27. Gaseous product; 28. Liquid product. Detailed Implementation

[0058] The present application will now be described in further detail with reference to the accompanying drawings and embodiments. Through these descriptions, the features and advantages of the present application will become clearer and more apparent.

[0059] The term “exemplary” as used herein means “serving as an example, embodiment, or illustration.” Any embodiment illustrated herein as “exemplary” is not necessarily to be construed as superior to or better than other embodiments. Although various aspects of embodiments are shown in the accompanying drawings, the drawings are not necessarily drawn to scale unless specifically indicated otherwise.

[0060] Furthermore, the technical features involved in the different embodiments of this application described below can be combined with each other as long as they do not conflict with each other.

[0061] This invention provides a method for refining gasoline, comprising:

[0062] (1) The gasoline raw material is cut into light gasoline, medium gasoline and heavy gasoline. The first cutting point for cutting light gasoline and medium gasoline is 50-90℃, and the second cutting point for cutting medium gasoline and heavy gasoline is 130-150℃. The light gasoline and heavy gasoline obtained from the cutting are the first gasoline raw material, and the medium gasoline is the second gasoline raw material.

[0063] (2) The mixture of the first gasoline feedstock and hydrogen is fed into the first moving bed reactor filled with an adsorption desulfurization catalyst for desulfurization adsorption and hydrogenation refining to obtain the first oil and gas product. The mixture of the second gasoline feedstock and hydrogen is fed into the second moving bed reactor filled with an adsorption desulfurization catalyst for desulfurization adsorption and hydrogenation refining to obtain the second oil and gas product.

[0064] (3) The first oil and gas product and the second oil and gas product are introduced into the oil and gas separation device separately or together to separate the oil and gas into gas products and obtain liquid refined gasoline products.

[0065] (4) The desulfurization catalyst to be regenerated after the reaction in the first moving bed reactor is introduced into the first regenerator for regeneration and reduction to obtain the first regenerated catalyst, and the first regenerated catalyst is returned to the first moving bed reactor; the desulfurization catalyst to be regenerated after the reaction in the second moving bed reactor is introduced into the second regenerator for regeneration and reduction to obtain the second regenerated catalyst, and the second regenerated catalyst is returned to the second moving bed reactor.

[0066] This invention relates to a method for refining gasoline, the method comprising: cutting gasoline into light fraction, middle fraction and heavy fraction, wherein the light fraction and heavy fraction are subjected to continuous desulfurization reaction in a first moving bed reactor under the action of an adsorption desulfurization catalyst, and the deactivated adsorption desulfurization catalyst is continuously regenerated and reduced in a moving bed regeneration system. The middle fraction undergoes desulfurization in a second moving bed reactor while avoiding aromatic saturation. Then, the first gasoline, mixed with hydrogen, contacts the continuously flowing, downward-flowing adsorption desulfurization catalyst in the moving bed reactor to undergo a desulfurization reaction. The products are withdrawn from the moving bed reactor, while the deactivated catalyst is removed and sent to the first moving bed regeneration system to restore its activity. This process is then continuously returned to the reactor, achieving a cyclical reaction-regeneration cycle. Similarly, the second gasoline, mixed with hydrogen, contacts the continuously flowing, downward-flowing adsorption desulfurization catalyst in the moving bed reactor to undergo a desulfurization reaction. The products are withdrawn from the moving bed reactor, while the deactivated catalyst is removed and sent to the second moving bed regeneration system to restore its activity. This process is then continuously returned to the reactor, achieving a cyclical reaction-regeneration cycle. This method of the present invention can deeply remove sulfur and nitrogen impurities from hydrocarbon oils, achieving complete saturation removal of olefins while minimizing or even increasing aromatic loss. It also solves the problem of catalyst regeneration after deactivation, improves catalyst stability during the reaction process, and significantly reduces the requirements for catalyst wear index.

[0067] This invention utilizes a moving bed for desulfurization and adsorption refining of gasoline feedstock. The main features of the moving bed are: (1) continuous movement of solid particles; (2) a wide range of particle sizes of catalyst solid particles; (3) a wide range of contact time between catalyst solid particles and fluid; (4) a near-plug flow between catalyst solid particles and fluid, resulting in high reaction efficiency; and (5) high thermal utilization rate of countercurrent contact.

[0068] The moving bed reactor technology is used for gasoline hydrorefining and combined with moving bed catalyst regeneration. By controlling the continuous reaction and deactivation of the catalyst during the movement process, and removing it from the reactor in a timely manner to be sent to the regeneration system for regeneration and reduction and recycling, the catalyst can maintain stable activity during the reaction process. This not only achieves full desulfurization of catalytic cracking gasoline, but also facilitates continuous production and sustained stability of catalyst activity during the reaction process.

[0069] In one embodiment, in step (1), the sulfur content of the gasoline feedstock is above 10 micrograms / gram, preferably above 30 micrograms / gram;

[0070] The nitrogen content is above 10 micrograms / gram, preferably above 20 micrograms / gram;

[0071] The olefin mass fraction is 5%-50%, preferably 10%-45%;

[0072] The aromatic hydrocarbon mass fraction is above 20%-90%, preferably 30%-80%;

[0073] Preferably, the gasoline feedstock is selected from one or more of catalytic cracking gasoline, reformed gasoline, or steam cracking gasoline.

[0074] In one embodiment, in step (2), the first gasoline feedstock, the second gasoline feedstock, and / or hydrogen are preheated before entering the moving bed reactor, and the preheating temperature is 200-550°C.

[0075] In one embodiment, in step (2), the reaction conditions in the first moving bed reactor are: reaction temperature of 350–550°C, reaction pressure of 0.5–5 MPa, and weight hourly space velocity of 0.1–100.0 h⁻¹. -1 The adsorption desulfurization catalyst moves at a velocity of 0.02–5.00 m / h in the first moving bed reactor, and the molar ratio of hydrogen to the first gasoline feedstock is 0.2–20.0; and / or

[0076] The reaction conditions in the second moving bed reactor are: reaction temperature 300–450℃, reaction pressure 1.5–5 MPa, and weight hourly space velocity 0.1–100.0 h⁻¹. -1The adsorption desulfurization catalyst moves at a speed of 0.02–5.00 m / h in the second moving bed reactor, and the molar ratio of hydrogen to the first gasoline feedstock is 0.2–20.0.

[0077] According to the present invention, the catalyst moving speed in the reactor is controlled at 0.02 to 5.00 m / hr, preferably at 0.05 to 4.00 m / hr. Combined with the corresponding reaction conditions, the catalyst can fully exert its catalytic activity by contacting the reactants while moving slowly. On the other hand, since the catalyst moving speed in the moving bed is much slower than in the fluidized bed reactor, the requirement for the catalyst wear resistance index is lower, and the range of catalysts that can be selected is much wider than that in the fluidized bed reactor.

[0078] The key to the design of this invention lies in the organic combination of moving bed reactor operation and moving bed regeneration system operation. The moving bed reactor, moving bed regeneration system and liquefied gas heating device involved in the implementation are all conventional devices in the field, and their specific working principles are also well known. The catalyst used is any catalyst that can achieve adsorption desulfurization of liquefied gas, especially some highly active and highly selective adsorption desulfurization catalysts.

[0079] In one specific embodiment, the method of the present invention may include the following steps:

[0080] (1) Cut the gasoline raw material into light, medium and heavy gasoline, wherein the first cutting point is 50-90℃ and the second cutting point is 130-150℃; preheat the first gasoline raw material, the second gasoline raw material of medium gasoline, and the hydrogen source, which are a mixture of light and heavy gasoline, to 200-550℃;

[0081] (2) At least a portion of the adsorption desulfurization catalyst is lifted to the upper part or top of the first moving bed reactor and fed into the reactor; while the adsorption desulfurization catalyst is fed into the first moving bed reactor, the mixture of the heated first gasoline feedstock and hydrogen is fed into the moving bed reactor, so that the adsorption desulfurization catalyst undergoes an adsorption desulfurization reaction during its downward movement. The reaction conditions in the moving bed reactor are controlled as follows: reaction temperature is 350-550℃, reaction pressure is 0.5-5MPa, weight hourly space velocity is 0.1-100.0h-1, the moving speed of the adsorption desulfurization catalyst in the first moving bed reactor is 0.02-5.00m / h, and the molar ratio of hydrogen to the first gasoline feedstock is 0.2-20.0.

[0082] (3) At least another portion of the adsorption desulfurization catalyst is lifted to the upper part or top of the second moving bed reactor and fed into the reactor; while the adsorption desulfurization catalyst is fed into the second moving bed reactor, the mixture of the heated second gasoline feedstock and hydrogen is fed into the moving bed reactor, so that the adsorption desulfurization catalyst undergoes an adsorption desulfurization reaction during its downward movement. The reaction conditions in the moving bed reactor are controlled as follows: reaction temperature 300-450℃, reaction pressure 1.5-5MPa, and weight hourly space velocity 0.1-100.0h. -1 The adsorption desulfurization catalyst moves at a speed of 0.02–5.00 m / h in the second moving bed reactor, and the molar ratio of hydrogen to the first gasoline feedstock is 0.2–20.0.

[0083] (4) The first and second products of the above adsorption desulfurization reaction are taken out of the first and second moving bed reactors for post-processing, while the adsorption desulfurization catalyst that has moved to the bottom of the reactor is taken out from the outlet at the bottom of the reactor.

[0084] (5) The adsorption desulfurization catalyst drawn from the lower or bottom outlet of the moving bed reactor is lifted to the upper or top of the first or second regeneration system of the adsorption desulfurization catalyst moving bed and enters the regeneration system.

[0085] (6) The adsorption desulfurization catalyst entering the first moving bed regeneration system and the second moving bed regeneration system is regenerated by contacting and reacting with the regeneration gas. The regeneration conditions are: regeneration temperature of 300-500℃, regeneration pressure of 0.1-2.0MPa, and regeneration gas is a mixture of oxygen and inactive gas with an oxygen volume content of 0.1-21.0%. After complete regeneration, the catalyst is reduced by contacting and reacting with reducing gas in the regeneration system. The reduction conditions are: reduction temperature of 260-400℃, reduction pressure of 0.1-2.0MPa, and reducing gas is a gas with a hydrogen volume content of at least 40%.

[0086] The regenerated and reduced catalyst is drawn out from the lower or bottom outlet of the regeneration system and returned to the reactor from the upper or top of the moving bed reactor through pipelines for continuous recycling.

[0087] In one embodiment, in step (3), the oil-gas separation temperature in the first oil-gas separator is 30–150°C, and the oil-gas separation pressure is 0.5–4 MPa; and / or

[0088] The oil-gas separation temperature in the second oil-gas separator is 50–200℃, and the oil-gas separation pressure is 0.5–5 MPa.

[0089] In one implementation, in step (4), the regeneration conditions of the first regenerator and / or the second regenerator are:

[0090] The regeneration temperature is 300–550℃, and the regeneration pressure is 0.1–2.0 MPa.

[0091] Preferably, the oxygen volume content in the regenerated gas is 0.1% to 21.0%, and air is preferred.

[0092] In one implementation, in step (4), the reduction conditions of the first regenerator and / or the second regenerator are:

[0093] The reduction temperature is 260–450℃, and the reduction pressure is 0.1–2.0 MPa;

[0094] Preferably, the hydrogen volume content in the reducing gas is at least 40%.

[0095] In one embodiment, in step (2), the adsorption desulfurization catalyst includes a support and a transition metal active component supported on the support;

[0096] Preferably, the support comprises zinc oxide, alumina, silica, and molecular sieve; and / or the transition metal active component is selected from one or more of cobalt, nickel, iron, manganese, copper, molybdenum, tungsten, silver, tin, and vanadium;

[0097] More preferably, the support contains 20-85 wt% zinc oxide, 5-85 wt% alumina, 5-85 wt% silica, and 5-35 wt% molecular sieve; the content of the transition metal active component accounts for 5-30 wt% of the total weight of the hydrorefining catalyst.

[0098] More preferably, the molecular sieve is a ZSM series molecular sieve, a Y-type molecular sieve, or a Beta-type molecular sieve;

[0099] More preferably, the molecular sieve is one in which Na has been replaced by ammonia exchange. + Ions, and molecular sieves that have been calcined at 450-700℃ for 1-10 hours.

[0100] The present invention also provides a gasoline refining system, comprising:

[0101] The raw material cutting unit includes:

[0102] A gasoline cutting tower is used to cut gasoline feedstock into light gasoline, medium gasoline and heavy gasoline. It is equipped with a gasoline feedstock inlet, a light gasoline outlet, a medium gasoline outlet and a heavy gasoline outlet.

[0103] The reaction unit includes:

[0104] The first moving bed reactor is used for desulfurization, adsorption, and hydrorefining of light gasoline and heavy gasoline. It is equipped with a first gasoline feedstock inlet, a first oil and gas product outlet, a first spent catalyst outlet, and a first regenerated catalyst inlet. The first gasoline feedstock inlet is connected to the light gasoline outlet and the heavy gasoline outlet of the gasoline cutting tower.

[0105] The second moving bed reactor is used for desulfurization and adsorption hydrogenation refining of medium-grade gasoline. It is equipped with a second gasoline feedstock inlet, a second oil and gas product outlet, a second unused catalyst outlet, and a second unused catalyst inlet. The second gasoline feedstock inlet is connected to the medium-grade gasoline outlet of the gasoline cutting tower.

[0106] The oil-gas separation unit includes:

[0107] The first oil-gas separation device is used to separate the first oil-gas product into oil and gas. It is provided with a first oil-gas product inlet, a first gas product outlet and a first liquid product outlet. The first oil-gas product inlet is connected to the first oil-gas product outlet of the first moving bed reactor.

[0108] The second oil-gas separation device is used to separate the second oil-gas product from the oil-gas product. It is provided with a second oil-gas product inlet, a second gas product outlet and a second liquid product outlet. The second oil-gas product inlet is connected to the second oil-gas product outlet of the second moving bed reactor.

[0109] Optional product mixing unit, including:

[0110] A mixer for mixing a first liquid product and a second liquid product is provided with one or more liquid product inlets and a refined gasoline product outlet, wherein the liquid product inlets are connected to the first liquid product outlet of the first oil-gas separator and the second liquid product outlet of the second moving bed reactor.

[0111] In one specific embodiment, the oil-gas separation unit is provided with only one oil-gas separation device for separating the first oil-gas product and the second oil-gas product.

[0112] In one embodiment, the raw material cutting unit further includes an optional raw material mixer for mixing light gasoline and heavy gasoline as a first gasoline raw material.

[0113] In one embodiment, the first moving bed reactor and / or the second moving bed reactor are axial moving bed reactors, in which the gasoline feedstock and hydrogen mixture undergo adsorption desulfurization and hydrogenation refining reaction with the adsorption desulfurization catalyst through co-current or counter-current contact.

[0114] In one embodiment, the first moving bed reactor and / or the second moving bed reactor are radial moving bed reactors;

[0115] Preferably, the radially moving bed reactor is cylindrical, with a central tube, an inner annular tube, and an outer annular tube arranged radially outward from its central axis. The inner annular gap between the inner annular tube and the central tube is the catalyst moving bed, and the outer annular gap between the outer annular tube and the inner annular tube is the reactant channel. The central tube is the product channel, allowing gasoline feedstock and hydrogen to mix and enter through the reactant channel. The mixture then enters through the reactant channel and undergoes cross-flow contact with the catalyst moving downward in the catalyst moving bed along the radial direction of the reactor, resulting in an adsorption desulfurization and hydrorefining reaction. The reacted oil and gas enter the central tube and are then drawn out.

[0116] In one embodiment, a catalyst moving bed is provided in the middle of the first moving bed reactor and / or the second moving bed reactor, and a reactant channel is provided on one side of the catalyst moving bed and a product channel is provided on the other side, so that the mixture of gasoline feedstock and hydrogen enters from the reactant channel, enters the reactor laterally, and undergoes adsorption desulfurization reaction by cross-flow contact with the catalyst moving downward in the catalyst moving bed, and the gasoline after reaction is drawn out from the product channel.

[0117] The moving bed reactor used in this invention can be an axial moving bed reactor that enables the reaction feedstock to move along the axial direction, or a radial moving bed reactor that enables the reaction feedstock to move in the radial or transverse direction, or other forms of moving bed reactor; correspondingly, the contact mode between the catalytic cracking gasoline feedstock and the adsorption desulfurization catalyst in the reactor can be countercurrent contact, cocurrent contact, or cross-flow contact.

[0118] In one embodiment, the reaction unit further includes at least one heating device for heating the first gasoline feedstock, the second gasoline feedstock, and / or hydrogen.

[0119] In one embodiment, the first moving bed reactor and / or the second moving bed reactor are single-stage or multi-stage reactors;

[0120] Preferably, the first moving bed reactor and / or the second moving bed reactor are multi-stage reactors, wherein the multi-stage reactors are connected in series, parallel or mixed.

[0121] More preferably, when the multi-stage reactors are connected in series, the multi-stage reactors are arranged horizontally side by side or vertically overlapping.

[0122] The present invention can also use a single-stage or higher moving bed reactor to realize the adsorption desulfurization reaction of catalytic cracking gasoline; when using a single-stage or higher reactor, (two or more sets) of reactors are operated in series or in parallel.

[0123] Depending on the specific conditions and needs of the raw materials and the adsorption desulfurization catalyst, the heating of the raw materials is achieved through at least one heating device. That is, it can be achieved through one-stage heating, or through two or more stages of heating treatment; for two or more stages of heating, two or more sets of heating devices can be connected in parallel or in series.

[0124] Figure 1 A flowchart of a specific embodiment of the present invention is shown, from... Figure 1 As can be seen from the above, the catalytic cracking gasoline adsorption desulfurization method provided by the present invention may include the following steps:

[0125] In the gasoline cutting tower 2, gasoline feedstock 1 is cut to obtain light gasoline 3, medium gasoline 4, and heavy gasoline 5. The gasoline described in this invention includes one or more of catalytic cracking gasoline, reformed gasoline, and steam cracking gasoline. Light gasoline 3 and heavy gasoline 5 are used as the first gasoline feedstock, and medium gasoline 4 is used as the second gasoline feedstock. The gasoline feedstock, along with the first hydrogen source 6 and the second hydrogen source 7, are heated to 200–550°C by a heating device (not shown in the figure) and then introduced into the first moving bed reactor 8 and the second moving bed reactor 9, respectively. This heating device can be a single unit (one-stage heating) or multiple units (multi-stage heating). For multi-stage heating, two or more heating devices can be operated in parallel or in series.

[0126] The adsorption desulfurization and hydrogenation refining catalyst is lifted through pipelines to the top or top of the moving bed reactor and enters the reactor. In continuous production, the adsorption desulfurization and hydrogenation refining catalyst is recycled from the moving bed catalyst regeneration system and then sent to the reactor through the lifting pipeline.

[0127] The heated first gasoline feedstock, along with hydrogen from the first hydrogen source 6, enters the first moving bed reactor 8 and comes into contact with the slowly moving adsorption desulfurization and hydrorefining catalyst to undergo an adsorption desulfurization and hydrorefining reaction. The reaction conditions are: reaction temperature of 350–550°C, reaction pressure of 0.5–5 MPa, weight hourly space velocity of 0.1–100.0 h⁻¹, moving speed of the adsorption desulfurization and hydrorefining catalyst in the moving bed reactor of 0.02–1.00 m / h, and molar ratio of hydrogen to the first gasoline feedstock of 0.2–20.0. The moving speed of the catalyst within the above range can be determined according to the specific characteristics of the catalyst and the specifications of the reactor, so that the activity of the catalyst is basically fully utilized when it is removed from the reactor, and regeneration can be carried out in a timely manner. After the first gasoline feedstock reacts under the above reaction conditions, the first oil and gas product 22 after the adsorption desulfurization and hydrorefining reaction is led out of the reactor and enters the first high-pressure separator 12 for oil and gas separation. The first gaseous product 23 obtained by separation is discharged from the separator, and the first liquid product 14 enters the mixer 16.

[0128] The heated second gasoline feedstock, along with hydrogen from the second hydrogen source 7, enters the second moving bed reactor and comes into contact with a slowly moving adsorption desulfurization and hydrorefining catalyst to undergo a refining reaction. The reaction conditions are: reaction temperature of 300–450°C, reaction pressure of 1.5–5 MPa, weight hourly space velocity of 0.1–100.0 h⁻¹, moving speed of the adsorption desulfurization and hydrorefining catalyst in the second moving bed reactor of 0.02–1.00 m / h, and molar ratio of hydrogen to the first gasoline feedstock of 0.2–20.0. The moving speed of the catalyst within the above range can be determined according to the specific characteristics of the catalyst and the specifications of the reactor, so that the activity of the catalyst is basically fully utilized when it is removed from the reactor, and regeneration can be carried out in a timely manner. After the second gasoline feedstock reacts under the above reaction conditions, the second oil and gas product 24 after the refining reaction is led out of the reactor and enters the second high-pressure separator 13 for oil and gas separation. The separated second gaseous product 25 is discharged from the separator, and the second liquid product 15 enters the mixer 16.

[0129] like Figure 2 As shown, in another embodiment, the first oil and gas product 22 and the second oil and gas product 24 after the refining reaction enter the high-pressure separator 26 for oil and gas separation. The separated gas product 27 is discharged from the separator, and the liquid product 28 enters the mixer 16.

[0130] In mixer 16, the first liquid product 14 and the second liquid product 15 are mixed to obtain the refined gasoline product 17.

[0131] The adsorption desulfurization and hydrorefining catalyst entering from the top or top of the first moving bed reactor 8 and the second moving bed reactor 9 reacts with the catalytic cracking gasoline while moving slowly downwards at an appropriate speed. The first and second pre-reacting agents 18 and 20 after the reaction are drawn out from the catalyst outlet at the bottom or bottom of the reactor (at this time, the catalyst activity has been basically lost).

[0132] The adsorption desulfurization and hydrogenation refining catalyst drawn from the lower or bottom catalyst outlet of the first moving bed reactor 8 and the second moving bed reactor 9 is lifted through pipelines to the upper or top of the moving bed regeneration system (first regenerator 10 and second regenerator 11) and enters the moving bed regeneration system.

[0133] The moving bed regeneration system includes catalyst regeneration and reduction reaction zones. Adsorption desulfurization catalyst (lost activity) entering from the top or upper part of the regeneration system reacts with regeneration gas and reducing gas respectively to restore activity, and then slowly moves downwards through the regeneration system. The regeneration conditions achieved by the catalyst reacting with the regeneration gas in the moving bed regeneration system are: regeneration temperature 300–500℃, regeneration pressure 0.1–2.0 MPa, and the regeneration gas being a mixture of oxygen and inactive gas with an oxygen volume content of 0.1–21.0%. After complete regeneration, the catalyst reacts with the reducing gas in the regeneration system to achieve catalyst reduction. The reduction conditions are: reduction temperature 260–400℃, reduction pressure 0.1–2.0 MPa, and the reducing gas being a gas with a hydrogen volume content of at least 40%.

[0134] The regenerated and activated catalyst (first regenerator 19 and second regenerator 21) is led out from the lower or bottom outlet of the regeneration system and enters the catalyst riser pipe connected to the upper or top of the reactor to return to the reactor, thereby realizing the continuous cycle of the catalyst "reaction-regeneration" process.

[0135] Note: In the claims and description of this invention, the terms "moving bed reactor" and "reactor" should be understood as "moving bed reactor," and "moving bed regeneration system" and "regeneration system" should be understood as "moving bed regeneration system."

[0136] The DCC gasoline feedstock used in the examples and comparative examples was obtained from the 2.2 million tons / year catalytic cracking unit of CNOOC Ningbo Daxie Petrochemical Co., Ltd., and its properties are listed in Table 1. The adsorption desulfurization and hydrorefining catalyst was FCAS-M (produced by Nanjing Catalyst Branch of China Petroleum & Chemical Corporation), with zinc oxide, silica, alumina and ZSM-5 as supports and Ni as a promoter.

[0137] Example 1

[0138] Gasoline feedstock undergoes adsorption desulfurization in a small continuous moving bed reactor, alternating with GCAS-2. The adsorption desulfurization and hydrorefining process conditions and the properties of the fitted product are shown in Table 2. Table 2 shows that the product has a sulfur content of 6.8 μg / g, an olefin loss of 2.3%, and the desulfurization adsorbent can operate continuously for 1-3 years.

[0139] Catalytic cracking gasoline is split into light gasoline, medium gasoline and heavy gasoline (the first cutting point is 60°C and the second cutting point is 135°C). Light gasoline and heavy gasoline are mixed as the first gasoline feedstock and medium gasoline is used as the second gasoline feedstock.

[0140] In a small continuous moving bed reactor, a first gasoline feedstock and a first hydrogen source are alternately contacted with a first adsorption desulfurization and hydrorefining catalyst to carry out a refining, desulfurization, and denitrification reaction, yielding a first oil and gas product after the reaction; the preheating temperature of the first gasoline feedstock and / or the hydrogen source is 400°C; the hydrorefining reaction temperature is 430°C; the hydrorefining reaction pressure is 3.0 MPa; and the weight hourly space velocity (WHSV) of the hydrocarbon oil is 2.5 h⁻¹. -1 The hydrogen-to-oil molar ratio is 1.0; the hydrogen source is high-purity hydrogen with a hydrogen content of 99.99% by volume; the catalyst moves at a speed of 2 m / h in the first moving bed reactor; the first oil and gas products after the reaction are separated in the first high-pressure separator at a separation temperature of 140°C and a separation pressure of 2.5 MPa.

[0141] The second gasoline feedstock and the second hydrogen source are subjected to a refining, desulfurization, and denitrification reaction in alternating contact with the second refining catalyst to obtain the second oil and gas product after the reaction; the preheating temperature of the hydrocarbon oil and / or the hydrogen source is 400°C; the temperature of the hydrorefining reaction is 400°C; the pressure of the hydrorefining reaction is 2.5 MPa; and the weight hourly space velocity of the hydrocarbon oil is 2.5 h⁻¹. -1 The hydrogen-to-oil molar ratio is 0.5; the hydrogen source is high-purity hydrogen with a hydrogen content of 99.99% by volume; the catalyst moves at a speed of 3 m / h in the second moving bed reactor; the first oil and gas product after the reaction is separated into oil and gas in the second high-pressure separator at a separation temperature of 130°C and a separation pressure of 3.2 MPa.

[0142] The first liquid product separated in the first high-pressure separator and the second liquid product separated in the second high-pressure separator are mixed in a mixer to obtain refined gasoline product.

[0143] The regenerated materials obtained from the first moving bed reactor and the second moving bed reactor are respectively fed into the first regenerator and the second regenerator for regeneration and reduction. The regeneration conditions include: a regeneration temperature of 550°C; a regeneration pressure of 0.1 MPa; a regeneration time of 120 minutes; and air as the regeneration gas. The reduction conditions include: a reduction temperature of 430°C; a reduction pressure of 0.1 MPa; a reduction time of 60 minutes; and high-purity hydrogen gas containing 99.99% by volume of hydrogen as the hydrogen atmosphere used for reduction.

[0144] Comparative Example 1

[0145] FCAS-M was used as a refining catalyst, and its refining activity on feedstock A was investigated in a small fixed-bed reactor. The reaction conditions were as follows: 16 g of refining catalyst was loaded into the reactor, and reduction was carried out for 1 h at a pressure of 3.0 MPa, a temperature of 400 °C, and a hydrogen flow rate of 16 L / h. Then, feedstock A was used as the reactant, and the reaction was carried out at a pressure of 3.0 MPa, a temperature of 300 °C, a hydrogen-to-oil molar ratio of 2.0, and a WHSV of 2.5 h. -1 The reaction was carried out under certain conditions, and the properties of the purified product are shown in Table 2.

[0146] Table 1 Properties of DCC Gasoline Feedstock

[0147]

[0148] Table 2 Properties of Refined Products

[0149]

[0150]

[0151] As can be seen from Table 2, compared with the fixed-bed reactor of Comparative Example 1, the moving-bed reactor of Example 1 achieves deep desulfurization, denitrification, and olefin saturation while significantly reducing the amount of aromatics saturation.

[0152] The present application has been described above with reference to preferred embodiments; however, these embodiments are merely exemplary and illustrative. Various substitutions and modifications can be made to the present application based on these embodiments, all of which fall within the protection scope of the present application.

Claims

1. A method for refining gasoline, comprising: (1) The gasoline raw material is cut into light gasoline, medium gasoline and heavy gasoline. The first cutting point for cutting light gasoline and medium gasoline is 50-90℃, and the second cutting point for cutting medium gasoline and heavy gasoline is 130-150℃. The light gasoline and heavy gasoline obtained from the cutting are the first gasoline raw material, and the medium gasoline is the second gasoline raw material. (2) The mixture of the first gasoline feedstock and hydrogen is fed into the first moving bed reactor filled with an adsorption desulfurization catalyst for desulfurization adsorption and hydrogenation refining to obtain the first oil and gas product. The mixture of the second gasoline feedstock and hydrogen is fed into the second moving bed reactor filled with an adsorption desulfurization catalyst for desulfurization adsorption and hydrogenation refining to obtain the second oil and gas product. (3) The first oil and gas product and the second oil and gas product are introduced into the oil and gas separation device separately or together to separate the gas product and obtain the liquid refined gasoline product. (4) The desulfurization catalyst to be regenerated after the reaction in the first moving bed reactor is introduced into the first regenerator for regeneration and reduction to obtain the first regenerated catalyst, and the first regenerated catalyst is returned to the first moving bed reactor; the desulfurization catalyst to be regenerated after the reaction in the second moving bed reactor is introduced into the second regenerator for regeneration and reduction to obtain the second regenerated catalyst, and the second regenerated catalyst is returned to the second moving bed reactor.

2. The method according to claim 1, characterized in that, In step (1), the sulfur content of the gasoline feedstock is above 10 micrograms / gram, preferably above 30 micrograms / gram; The nitrogen content is above 10 micrograms / gram, preferably above 20 micrograms / gram; The olefin mass fraction is 5%-50%, preferably 10%-45%; The aromatic hydrocarbon mass fraction is above 20%-90%, preferably 30%-80%; Preferably, the gasoline feedstock is selected from one or more of catalytic cracking gasoline, reformed gasoline, or steam cracking gasoline.

3. The method according to claim 1, characterized in that, In step (2), the first gasoline feedstock, the second gasoline feedstock and / or hydrogen are preheated before entering the moving bed reactor, and the preheating temperature is 200-550°C.

4. The method according to claim 1, characterized in that, In step (2), the reaction conditions in the first moving bed reactor are: reaction temperature of 350–550℃, reaction pressure of 0.5–5 MPa, and weight hourly space velocity of 0.1–100.0 h⁻¹. -1 The adsorption desulfurization catalyst moves at a velocity of 0.02–5.00 m / h in the first moving bed reactor, and the molar ratio of hydrogen to the first gasoline feedstock is 0.2–20.0; and / or The reaction conditions in the second moving bed reactor are: reaction temperature 300–450℃, reaction pressure 1.5–5 MPa, and weight hourly space velocity 0.1–100.0 h⁻¹. -1 The adsorption desulfurization catalyst moves at a speed of 0.02–5.00 m / h in the second moving bed reactor, and the molar ratio of hydrogen to the first gasoline feedstock is 0.2–20.

0.

5. The method according to claim 1, characterized in that, In step (3), the oil-gas separation temperature in the first oil-gas separator is 30–150°C, and the oil-gas separation pressure is 0.5–4 MPa; and / or The oil-gas separation temperature in the second oil-gas separation device is 50–200℃, and the oil-gas separation pressure is 0.5–4MPa.

6. The method according to claim 1, characterized in that, In step (4), the regeneration conditions of the first regenerator and / or the second regenerator are as follows: The regeneration temperature is 300–550℃, and the regeneration pressure is 0.1–2.0 MPa. Preferably, the oxygen volume content in the regenerated gas is 0.1% to 21.0%, and air is preferred.

7. The method according to claim 1, characterized in that, In step (4), the reduction conditions for the first regenerator and / or the second regenerator are as follows: The reduction temperature is 260–450℃, and the reduction pressure is 0.1–2.0 MPa; Preferably, the hydrogen volume content in the reducing gas is at least 40%.

8. The method according to claim 1, characterized in that, In step (2), the adsorption desulfurization catalyst includes a support and a transition metal active component supported on the support; Preferably, the support comprises zinc oxide, alumina, silica, and molecular sieve; and / or the transition metal active component is selected from one or more of cobalt, nickel, iron, manganese, copper, molybdenum, tungsten, silver, tin, and vanadium; More preferably, the support contains 20-85 wt% zinc oxide, 5-85 wt% alumina, 5-85 wt% silica, and 5-35 wt% molecular sieve; the content of the transition metal active component accounts for 5-30 wt% of the total weight of the hydrorefining catalyst. More preferably, the molecular sieve is a ZSM series molecular sieve, a Y-type molecular sieve, or a Beta-type molecular sieve; More preferably, the molecular sieve is one in which Na has been replaced by ammonia exchange. + Ions, and molecular sieves that have been calcined at 450-700℃ for 1-10 hours.

9. A gasoline refining system, comprising: The raw material cutting unit includes: A gasoline cutting tower is used to cut gasoline feedstock into light gasoline, medium gasoline and heavy gasoline. It is equipped with a gasoline feedstock inlet, a light gasoline outlet, a medium gasoline outlet and a heavy gasoline outlet. The reaction unit includes: The first moving bed reactor is used to desulfurize, adsorb, and hydrogenate light gasoline and heavy gasoline to obtain the first oil and gas product. It is provided with a first gasoline feedstock inlet, a first oil and gas product outlet, a first spent catalyst outlet, and a first regenerated catalyst inlet. The first gasoline feedstock inlet is connected to the light gasoline outlet and the heavy gasoline outlet of the gasoline cutting tower. The second moving bed reactor is used to desulfurize and adsorb hydrogenate the intermediate gasoline to obtain the second oil and gas product. It is equipped with a second gasoline feedstock inlet, a second oil and gas product outlet, a second unused catalyst outlet, and a second unused catalyst inlet. The second gasoline feedstock inlet is connected to the intermediate gasoline outlet of the gasoline cutting tower. The oil-gas separation unit includes: One or more oil-gas separation devices are used to separate a first oil-gas product and a second oil-gas product. The device is provided with an oil-gas product inlet, a gas product outlet and a liquid product outlet. The oil-gas product inlet is connected to the first oil-gas product outlet of the first moving bed reactor and the second oil-gas product outlet of the second moving bed reactor. An optional mixer is used to mix liquid products from multiple oil-gas separation units to obtain refined gasoline products, the mixer being connected to the liquid product outlet of the oil-gas separation unit.

10. The system according to claim 9, characterized in that, The raw material cutting unit also includes an optional raw material mixer for mixing light gasoline and heavy gasoline as a first gasoline raw material.

11. The system according to claim 9, characterized in that, The first moving bed reactor and / or the second moving bed reactor are axial moving bed reactors, in which the gasoline feedstock and hydrogen mixture undergo adsorption desulfurization and hydrogenation refining reaction with the adsorption desulfurization catalyst through co-current or counter-current contact.

12. The system according to claim 9, characterized in that, The first moving bed reactor and / or the second moving bed reactor are radial moving bed reactors; Preferably, the radially moving bed reactor is cylindrical, with a central tube, an inner annular tube, and an outer annular tube arranged radially outward from its central axis. The inner annular gap between the inner annular tube and the central tube is the catalyst moving bed, and the outer annular gap between the outer annular tube and the inner annular tube is the reactant channel. The central tube is the product channel, allowing gasoline feedstock and hydrogen to mix and enter through the reactant channel. The mixture then enters through the reactant channel and undergoes cross-flow contact with the catalyst moving downward in the catalyst moving bed along the radial direction of the reactor, resulting in an adsorption desulfurization and hydrorefining reaction. The reacted oil and gas enter the central tube and are then drawn out.

13. The system according to claim 9, characterized in that, A catalyst moving bed is provided in the middle of the first moving bed reactor and / or the second moving bed reactor. A reactant channel is provided on one side of the catalyst moving bed and a product channel is provided on the other side. The mixture of gasoline feedstock and hydrogen enters the reactor laterally through the reactant channel and undergoes cross-flow contact with the catalyst moving downward in the catalyst moving bed to carry out an adsorption desulfurization reaction. The gasoline after the reaction is drawn out through the product channel.

14. The system according to claim 9, characterized in that, The reaction unit also includes at least one heating device for heating the first gasoline feedstock, the second gasoline feedstock, and / or hydrogen.

15. The system according to claim 9, characterized in that, The first moving bed reactor and / or the second moving bed reactor are single-stage or multi-stage reactors; Preferably, the first moving bed reactor and / or the second moving bed reactor are multi-stage reactors, wherein the multi-stage reactors are connected in series, parallel or mixed. More preferably, when the multi-stage reactors are connected in series, the multi-stage reactors are arranged horizontally side by side or vertically overlapping.

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